US7485213B2 - Electrodeionization apparatus - Google Patents

Electrodeionization apparatus Download PDF

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Publication number
US7485213B2
US7485213B2 US10/535,035 US53503505A US7485213B2 US 7485213 B2 US7485213 B2 US 7485213B2 US 53503505 A US53503505 A US 53503505A US 7485213 B2 US7485213 B2 US 7485213B2
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Prior art keywords
compartments
desalting
anion
exchange resin
cation
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Expired - Fee Related, expires
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US10/535,035
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US20060037862A1 (en
Inventor
Masayuki Miwa
Shin Sato
Takayuki Moribe
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Kurita Water Industries Ltd
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Kurita Water Industries Ltd
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Assigned to KURITA WATER INDUSTRIES LTD. reassignment KURITA WATER INDUSTRIES LTD. ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: MIWA, MASAYUKI, MORIBE, TAKAYUKI, SATO, SHIN
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
    • B01D61/42—Electrodialysis; Electro-osmosis ; Electro-ultrafiltration; Membrane capacitive deionization
    • B01D61/44—Ion-selective electrodialysis
    • B01D61/46—Apparatus therefor
    • B01D61/48—Apparatus therefor having one or more compartments filled with ion-exchange material, e.g. electrodeionisation
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
    • B01D61/42—Electrodialysis; Electro-osmosis ; Electro-ultrafiltration; Membrane capacitive deionization
    • B01D61/44—Ion-selective electrodialysis
    • B01D61/46—Apparatus therefor
    • B01D61/50—Stacks of the plate-and-frame type
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J39/00—Cation exchange; Use of material as cation exchangers; Treatment of material for improving the cation exchange properties
    • B01J39/08—Use of material as cation exchangers; Treatment of material for improving the cation exchange properties
    • B01J39/16—Organic material
    • B01J39/18—Macromolecular compounds
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J41/00—Anion exchange; Use of material as anion exchangers; Treatment of material for improving the anion exchange properties
    • B01J41/08—Use of material as anion exchangers; Treatment of material for improving the anion exchange properties
    • B01J41/12—Macromolecular compounds
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J47/00—Ion-exchange processes in general; Apparatus therefor
    • B01J47/02—Column or bed processes
    • B01J47/04—Mixed-bed processes
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J47/00—Ion-exchange processes in general; Apparatus therefor
    • B01J47/02—Column or bed processes
    • B01J47/06—Column or bed processes during which the ion-exchange material is subjected to a physical treatment, e.g. heat, electric current, irradiation or vibration
    • B01J47/08—Column or bed processes during which the ion-exchange material is subjected to a physical treatment, e.g. heat, electric current, irradiation or vibration subjected to a direct electric current
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
    • C02F1/469—Treatment of water, waste water, or sewage by electrochemical methods by electrochemical separation, e.g. by electro-osmosis, electrodialysis, electrophoresis
    • C02F1/4693—Treatment of water, waste water, or sewage by electrochemical methods by electrochemical separation, e.g. by electro-osmosis, electrodialysis, electrophoresis electrodialysis
    • C02F1/4695—Treatment of water, waste water, or sewage by electrochemical methods by electrochemical separation, e.g. by electro-osmosis, electrodialysis, electrophoresis electrodialysis electrodeionisation
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/42—Treatment of water, waste water, or sewage by ion-exchange
    • C02F2001/427—Treatment of water, waste water, or sewage by ion-exchange using mixed beds
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
    • Y02A20/00—Water conservation; Efficient water supply; Efficient water use
    • Y02A20/124—Water desalination

Definitions

  • the present invention relates to an electrodeionization apparatus. More specifically, the present invention relates to an electrodeionization apparatus having excellent desalting capacity and operational stability even with a high loading of weak ions including CO 2 and silica.
  • JP 1782943 Japanese Patent No. 1782943
  • JP 2751090 JP 2699256.
  • JP 2699256 JP 1782943
  • multiple anion exchange membranes and cation exchange membranes are alternately arranged between a cathode and an anode to alternately form concentrating compartments and desalting compartments.
  • the desalting compartments are filled with an ion exchanger that is constituted of a mixed ion exchange resin of anion exchange resin and cation exchange resin, ion exchange fibers or the like.
  • an electrodeionization apparatus including concentrating compartments filled with an ion exchanger has also been proposed, as described in Japanese Patent Application Laid Open No. 2002-205069.
  • each kind of ion conducted into the desalting compartments reacts with the ion exchanger and moves in the ion exchanger along the direction of electrical potential gradient in a specific manner according to its affinity, concentration and mobility.
  • the ions further traverse the membranes to maintain all compartments electrically neutral.
  • the ions are removed from the desalting compartments and concentrated in the adjacent concentrating compartments because of the semipermeable property of the membranes and the directionality of electrical potential gradient. That is, the cations and the anions permeate through the cation exchange membranes and the anion exchange membranes, respectively, and are concentrated in the concentrating compartments. Therefore, the water produced from the desalting compartments can be recovered as deionized water (pure water).
  • the above electrodeionization apparatus is capable of efficiently implementing a desalting treatment without the requirement of regenerating the ion exchange resin. Therefore, the electrodeionization apparatus has the capability of continuously producing deionized water of extremely high purity.
  • Patent documents include:
  • Patent document 1 JP 1782943
  • Patent document 2 JP 2751090
  • Patent document 3 JP 2699256
  • Patent document 4 Japanese Patent Application Laid Open No. 2002-205069
  • the loading of weak ions including CO 2 and silica in the electrodeionization apparatus is high, i.e., when the concentration of the weak ions including CO 2 and silica in the water being treated is high or the amount of such water being treated is large, the quality of the deionized water produced is deteriorated as indicated by the specific resistivity thereof. Moreover, the electrical resistance of the system gets higher after long-term use, so that the operational stability of the apparatus is lowered.
  • Japanese Patent Application Laid Open No. 2002-205069 disclosed that the concentrating compartments can also be filled with an ion exchanger.
  • an electric conductor like an ion exchanger is filled in the concentrating compartments merely for maintaining the required current magnitude, so that the ratio of anion exchanger to cation exchanger of the ion exchanger is not particularly discussed. Therefore, as in the desalting compartments, a mixed ion exchange resin having the same “volume ratio of anion exchange resin to cation exchange resin” of 7:3 is filled in the concentrating compartments in the examples of Japanese Patent Application Laid Open No. 2002-205069.
  • one object of this invention is to provide an electrodeionization apparatus that has excellent desalting capacity and operational stability even when the loading of weak ions including CO 2 and silica is high.
  • the electrodeionization apparatus of this invention includes multiple anion exchange membranes and cation exchange membranes that are alternately arranged between a cathode and an anode to alternately form concentrating compartments and desalting compartments.
  • the concentrating compartments and the desalting compartments are filled with ion exchangers, and the filling ratio of anion exchanger to cation exchanger of the ion exchanger in the concentrating compartments is higher than that of the ion exchanger in the desalting compartments.
  • the cations in the treated water permeate the cation exchange membranes to be concentrated in the concentrating compartments and then removed.
  • the anions in the treated water permeate the anion exchange membranes to be concentrated in the concentrating compartments and then removed.
  • CO 2 and silica among the weak ions that are difficult to remove are converted to HCO 3 ⁇ and HSiO 3 ⁇ by the OH ⁇ ions generated from the hydrolysis reaction in the desalting compartments, and are emitted to the concentrating compartments.
  • the anionic species are most concentrated at the interfaces of the anion exchange membranes near the concentrating compartments because of the concentration polarization effect.
  • concentration polarization of HCO 3 ⁇ and HSiO 3 ⁇ having low mobility gets overly large, the electrical resistance of the system is raised making the removal of ions difficult. Therefore, the removal ratio of the ions is lowered in the prior art.
  • the electrodeionization apparatus of this invention preferably has multiple desalting compartments and concentrating compartments, wherein the anion/cation ratio of the ion exchanger in the concentrating compartments is preferably 75/25 to 95/5 in particular.
  • the ion exchanger filled in the concentrating compartments is preferably an ion exchange resin, wherein the crosslinking degree of the anion exchange resin is preferably 3-8% and that of the cation exchange resin is preferably 5-10%.
  • the anion exchange resin is preferably a thermostable anion exchange resin in particular.
  • the electrodeionization apparatus of this invention has excellent desalting capacity and operational stability even when the loading of weak ions including CO 2 and silica is high Accordingly, even when the ratio of the water introduction rate (L/h) into the desalting compartment to the effective area (dm 2 ) of the anion exchange membrane in the desalting compartment is 5 or higher, or when at least one of the following two conditions (1) and (2) is satisfied, good results can be obtained in some aspects including the desalting capacity and the electrical resistance by setting the current density to 300 mA/dm 2 or higher.
  • the condition (1) is that the ratio of the carbonate loading (mg-CO 2 /h) into the desalting compartment to the effective area (dm 2 ) of the anion exchange membrane in the desalting compartment is 80 or higher.
  • the condition (2) is that the ratio of the silica loading (mg-SiO 2 /h) into the desalting compartment to the effective area (dm 2 ) of the anion exchange membrane in the desalting compartment is 8 or higher.
  • FIG. 1 schematically illustrates a cross-sectional view of an electrodeionization apparatus according to a preferred embodiment of this invention.
  • FIG. 1 schematically illustrates a cross-sectional view of an electrodeionization apparatus according to the preferred embodiment of this invention.
  • the electro-deionization apparatus will be described in detail with reference to FIG. 1 .
  • multiple anion exchange membranes 13 and cation exchange membranes 14 are alternately arranged between two electrodes (an anode 11 and a cathode 12 ) to alternately form multiple concentrating compartments 15 and desalting compartments 16 .
  • the desalting compartments 16 and the concentrating compartments 15 are respectively filled with a mixed ion exchange resin of cation exchange resin 10 A and anion exchange resin 10 B.
  • the anode compartment is labeled with “17”, and the cathode compartment is labeled with “18”.
  • the anion/cation ratio of the mixed ion exchange resin filled in the concentrating compartments 15 is higher than that of the mixed ion exchange resin filled in the desalting compartments 16 . Therefore, as explained above, the motions of anions including HCO 3 ⁇ and HSiO 3 ⁇ are accelerated so that concentration polarization near the anion exchange membranes 13 is prevented. However, when the anion/cation ratio of the mixed ion exchange resin in the concentrating compartments 15 is overly high, concentration polarization of cations will occur at the concentrating interface on the side of the cation exchange membrane 14 in the concentrating compartment 15 .
  • the anion/cation ratio of the mixed ion exchange resin in the concentrating compartments 15 is generally 75/25-95/5, preferably 80/20-90/10 in particular.
  • the anion/cation ratio is defined as the volume ratio of the anion exchange resin to the cation exchange resin in their regenerated forms.
  • the ion exchanger filled in the concentrating compartments 15 is not restricted to ion exchange resin, and ion exchange fibers or a graft exchanger can also be used.
  • the ion exchanger is preferably an ion exchange resin in consideration of handling facility.
  • the crosslinking degree of the anion exchange resin is preferably 3-8% and that of the cation exchange resin is preferably 5-10%.
  • the crosslinking degree of respective ion exchange resin is lower than the corresponding lower limit, the mechanical strength of the same is weak.
  • the crosslinking degree of respective ion exchange resin is higher than the corresponding upper limit, the electrical resistance of the system is adversely raised.
  • the percentage of anion exchange resin in the ion exchange resin in the concentrating compartments 15 is high, degradation will occur after long-term operation raising the electrical resistance. That is, generally, when the ion exchange resins are oxidized/degraded in the presence of oxygen, for example, the anion exchange resin is degraded prior to the cation exchange resin. Therefore, when the percentage of anion exchange resin in the concentrating compartments 15 is high, it is preferable to use an anion exchange resin that has high resistance to oxidization/degradation and good thermostability.
  • the water supplied to the electrodeionization apparatus is generally some raw water like city water that has been treated with active carbon and reverse osmosis (RO) separation, wherein the electrical conductivity is 3-10 ⁇ S/cm, the concentration of CO 2 is 3-30 ppm and the concentration of silica is 0.2-1.0 ppm.
  • RO reverse osmosis
  • the anion/cation ratio of the ion exchange resin in the desalting compartments 16 is required to be 60/40-70/30.
  • the desalting compartments 16 are not restricted to fill with ion exchange resin, and other type of ion exchanger, such as ion exchange fibers or the like may also be used.
  • the water to be treated is conducted into the concentrating compartments 15 and the desalting compartments 16 in the electrodeionization apparatus of this invention.
  • the ions in the treated water conducted into the desalting compartments 16 the cations and the anions permeate the cation exchange membranes 14 and the anion exchange membranes 13 , respectively, and are concentrated in the concentration compartments 15 .
  • the water produced from the desalting compartments 16 is collected as deionized water.
  • concentrated water containing a high concentration of ions is output from the concentrating compartments 15 .
  • anode compartment 17 and the cathode compartment 18 are also introduced with electrode water, which is generally the effluent water (concentrated water) having a high concentration of ions from the concentrating compartments 15 for maintaining the electrical conductivity.
  • electrode water is generally the effluent water (concentrated water) having a high concentration of ions from the concentrating compartments 15 for maintaining the electrical conductivity.
  • the concentrated water having a high concentration of ions from the concentrating compartments 15 is generally divided into several portions.
  • a portion of the concentrated water is circulated to the inlet of the concentrating compartments 15 for increasing the recovery ratio of water.
  • Another portion is supplied to the inlet of the anode compartment 17 , and the remaining portion is discharged outside the system as wastewater for preventing ion concentration within the system.
  • the effluent water from the anode compartment 17 is supplied to the inlet of the cathode compartment 18 , and the effluent water from the cathode compartment 18 is discharged outside the system as wastewater.
  • the possibility of concentration polarization, especially that of weak ions including CO 2 and silica, occurring at the concentrating interface of the anion exchange membrane 13 in the concentrating compartment 15 increases with the increase in the following parameters.
  • One parameter is the amount of weak ions including CO 2 and silica conducted into the desalating compartments 16
  • Another parameter is the amount of weak ions including CO 2 and silica moving into the concentrating compartments 15 from the desalting compartments 16 through the anion exchange membranes 13 .
  • Still another parameter is the current density applied.
  • the electrodeionization apparatus of this invention wherein the anion/cation ratio of the ion exchanger in the concentrating compartments 15 is higher than that of the ion exchanger in the desalting compartments 16 , excellent desalting capacity and operational stability can be achieved even when the loading of weak ions is high.
  • the electrodeionization apparatus is stable in the aspects including desalting capacity and electric resistance even under the condition that the ratio of the carbonate loading (mg-CO 2 /h) into the desalting compartment 16 to the effective area (dm 2 ) of the anion exchange membrane 13 in the desalting compartment 16 is 80 or higher (or even 250-300), or that the ratio of the silica loading (mg-SiO 2 /h) into the desalting compartment 16 to the effective area (dm 2 ) of the anion exchange membrane 13 in the desalting compartment 16 is 8 or higher (or even 15-25), or that the current density is 300 mA/dm 2 or higher (or even 600-1200 mA/dm 2 ). Accordingly, the electrodeionization apparatus can be further compactified, which is quite attractive in consideration of economics.
  • the anode compartment 17 or the cathode compartment 18 can also be filled with an electric conductor or an ion exchanger like ion exchange resin.
  • An electrodeionization apparatus having a water-treating capacity of 1000 L/h is used, which is constituted of eight desalting compartments each having dimensions of 250 mm ⁇ 400 mms ⁇ 5 mm (effective width ⁇ height ⁇ thickness) and concentrating compartments each having a thickness of 2.5 mm.
  • the desalting compartments and the concentrating compartments are respectively filled with a mixed ion exchange resin described below.
  • the water supplied to the apparatus is city water that has been treated with active carbon and reverse osmosis (RO) separation.
  • the effective area (dm 2 ) of the anion exchange membrane in the desalting compartments of the electrodeionization apparatus is 10 dm 2 .
  • the water flow rate into the inlets of the desalting compartments is 1000 L/h, and that into the inlets of the concentrating compartments is 400 L/h.
  • the concentrated water flowing out of the concentrating compartments is divided into three portions, wherein a portion is discharged outside the system at a flow rate of 200 L/h, and another portion is sequentially conducted through the anode compartment and the cathode compartment and then discharged outside the system at a flow rate of 50 L/h. The remaining portion of the concentrated water is circulated to the inlets of the concentrating compartments.
  • the water introduction operation is continued under a current of 8 A for a month, wherein the conditions of water introduction are listed below.
  • the specific resistivity of the output water and the operation voltage after a month are listed in Table 1.
  • the specific resistivity and the operation voltage are stable and do not deviate from the values measured in the beginning.
  • the conditions of water introduction include:
  • Example 1 the water introduction operation is implemented as in Example 1 except that the anion/cation ratio of the mixed ion exchange resin filled in the concentrating compartments is varied as in Table 1.
  • Table 1 The specific resistivity of the output water and the operation voltage after a month in each example are listed in Table 1.
  • an electrodeionization apparatus can be provided with excellent desalting capacity and operational stability even when the loading of weak ions including CO 2 and silica is high.

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  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Water Supply & Treatment (AREA)
  • Engineering & Computer Science (AREA)
  • Organic Chemistry (AREA)
  • Health & Medical Sciences (AREA)
  • Urology & Nephrology (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Molecular Biology (AREA)
  • Electrochemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Hydrology & Water Resources (AREA)
  • Analytical Chemistry (AREA)
  • Environmental & Geological Engineering (AREA)
  • Separation Using Semi-Permeable Membranes (AREA)
  • Water Treatment By Electricity Or Magnetism (AREA)
US10/535,035 2002-11-15 2003-11-11 Electrodeionization apparatus Expired - Fee Related US7485213B2 (en)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
JP2002-332672 2002-11-15
JP2002332672A JP3956836B2 (ja) 2002-11-15 2002-11-15 電気脱イオン装置
PCT/IB2003/005042 WO2004047991A1 (ja) 2002-11-15 2003-11-11 電気脱イオン装置

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US20060037862A1 US20060037862A1 (en) 2006-02-23
US7485213B2 true US7485213B2 (en) 2009-02-03

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US (1) US7485213B2 (ko)
JP (1) JP3956836B2 (ko)
KR (1) KR100709693B1 (ko)
CN (1) CN100339161C (ko)
AU (1) AU2003276528A1 (ko)
CA (1) CA2503733C (ko)
GB (1) GB2409685B (ko)
TW (1) TWI257324B (ko)
WO (1) WO2004047991A1 (ko)

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US8671985B2 (en) 2011-10-27 2014-03-18 Pentair Residential Filtration, Llc Control valve assembly
US8961770B2 (en) 2011-10-27 2015-02-24 Pentair Residential Filtration, Llc Controller and method of operation of a capacitive deionization system
US9010361B2 (en) 2011-10-27 2015-04-21 Pentair Residential Filtration, Llc Control valve assembly
US9490418B2 (en) 2011-03-29 2016-11-08 Avago Technologies General Ip (Singapore) Pte. Ltd. Acoustic resonator comprising collar and acoustic reflector with temperature compensating layer
US9637397B2 (en) 2011-10-27 2017-05-02 Pentair Residential Filtration, Llc Ion removal using a capacitive deionization system
US9695070B2 (en) 2011-10-27 2017-07-04 Pentair Residential Filtration, Llc Regeneration of a capacitive deionization system

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JP4400218B2 (ja) * 2004-01-09 2010-01-20 栗田工業株式会社 電気式脱イオン装置及び脱イオン方法
US7892848B2 (en) * 2005-04-14 2011-02-22 Trovion Singapore Pte. Ltd., Co. Method of ion chromatography wherein a specialized electrodeionization apparatus is used
SG174801A1 (en) * 2006-06-22 2011-10-28 Siemens Water Tech Corp Electrodeionization apparatus and low scale potential water treatment
US20080067069A1 (en) 2006-06-22 2008-03-20 Siemens Water Technologies Corp. Low scale potential water treatment
JP4867720B2 (ja) * 2007-03-06 2012-02-01 栗田工業株式会社 純水製造方法及び装置
US8585882B2 (en) 2007-11-30 2013-11-19 Siemens Water Technologies Llc Systems and methods for water treatment
JP2010201361A (ja) * 2009-03-04 2010-09-16 Japan Organo Co Ltd 電気式脱イオン水製造装置及びこれを用いた脱イオン水の製造方法
JP2017140548A (ja) * 2016-02-08 2017-08-17 栗田工業株式会社 電気脱イオン装置の運転方法
JP7213006B2 (ja) * 2017-02-09 2023-01-26 栗田工業株式会社 導電性水溶液の製造装置及び導電性水溶液の製造方法
JP2019177328A (ja) * 2018-03-30 2019-10-17 栗田工業株式会社 電気脱イオン装置の運転方法
JP6627943B2 (ja) * 2018-10-02 2020-01-08 三菱ケミカルアクア・ソリューションズ株式会社 純水製造方法
JP2021037469A (ja) * 2019-09-03 2021-03-11 栗田工業株式会社 電気脱イオン装置及び脱イオン水の製造方法

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EP0870533A1 (en) 1997-04-10 1998-10-14 Asahi Glass Company Ltd. Apparatus for producing deionized water
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WO2002096807A2 (en) 2001-05-29 2002-12-05 United States Filter Corporation Electrodeionization apparatus and method

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EP0170895A2 (en) 1984-07-09 1986-02-12 Millipore Corporation Improved electrodeionization apparatus and method
JPH0472567A (ja) 1990-07-13 1992-03-06 Canon Inc 免疫的に活性な物質の測定方法および測定装置
JPH07236889A (ja) 1993-04-21 1995-09-12 Nippon Rensui Kk 純水製造装置
JPH07100391A (ja) 1993-10-05 1995-04-18 Ebara Corp 電気再生式連続イオン交換装置とその使用方法
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CA2503733C (en) 2008-08-19
JP3956836B2 (ja) 2007-08-08
US20060037862A1 (en) 2006-02-23
JP2004167291A (ja) 2004-06-17
WO2004047991A1 (ja) 2004-06-10
GB2409685B (en) 2006-06-28
CN1711136A (zh) 2005-12-21
AU2003276528A1 (en) 2004-06-18
TW200414922A (en) 2004-08-16
GB2409685A (en) 2005-07-06
TWI257324B (en) 2006-07-01
GB0507593D0 (en) 2005-05-18
CA2503733A1 (en) 2004-06-10
KR20050067224A (ko) 2005-06-30
KR100709693B1 (ko) 2007-04-19

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